CN1058514C - Combination process for producing fine quality catalytic cracking raw material - Google Patents
Combination process for producing fine quality catalytic cracking raw material Download PDFInfo
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- CN1058514C CN1058514C CN95103679A CN95103679A CN1058514C CN 1058514 C CN1058514 C CN 1058514C CN 95103679 A CN95103679 A CN 95103679A CN 95103679 A CN95103679 A CN 95103679A CN 1058514 C CN1058514 C CN 1058514C
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- wax tailings
- lubricating oil
- extract
- coking
- raffinate
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Abstract
The present invention relates to a combined process for producing a high quality catalytic cracking raw material, which is characterized in that coking and a lubricating oil extracting apparatus are combined to extract coked wax oil with lubricating oil extracted liquid so that the basic nitrogen gum content and the gelatine gum content of the coked wax oil are greatly reduced to provide a high quality raw material for a catalytic cracking apparatus. An additional set of extracting apparatus does not need to be established for the process flow of the present invention, a large amount of investment can be saved, and the consumption of a new solvent and the operation cost for recovery also do not need to be increased.
Description
The present invention is a kind of process integration of producing fine quality catalytic cracking raw material, or rather, is a kind of coking and lubricating oil extraction plant process integration, is about to the lubricating oil Extract and is used to extract wax tailings, to improve the quality of catalytically cracked material.
Wax tailings is one of important source material of catalytic cracking unit, but wherein contains more basic nitrogen compound and colloid, if directly advance catalytic cracking unit, will make the poisoning of catalyst inactivation, reduces the transformation efficiency of catalytic cracking, therefore must manage to remove.The way that solves has at present: hydrotreatment; Acid treatment; Change operational condition as improving temperature, dose oil ratio etc.; Mix the raw material that refining contains the low alkalinity nitride; Use high activated catalyst or the like.Aforesaid method respectively has its advantage, also has deficiency, as the hydrotreatment apparatus expensive, and acid treatment meeting etching apparatus, it is unreasonable economically to change operational condition, mixes the restriction that refining is subjected to raw material again.Solvent extraction then is considered to solution route preferably.
USP2,943,995 introduce employing two-stage coking technology, promptly use the aromatic hydrocarbons in first section coking distillate of selective solvent extracting; Send second section coker to carry out coking in the aromatic hydrocarbons of extracting out.USP4534854 discloses heavy oil fraction that coking fractional distillation column is told through solvent extraction or solvent deasphalting, be divided into two kinds of overhead products that contain high carbon residue and low carbon residue again, catalytically cracked material is made in the low all or part of recovery of carbon residue overhead product, high carbon residue overhead product circulation coking, this technology to carry surplus heavy oil fraction yield low be that catalytically cracked material reduces, and need build a cover solvent extraction or a solvent deasphalting unit, increase investment and process cost.
The objective of the invention is to overcome the shortcoming of prior art, propose a kind of coking and lubricating oil extraction plant process integration, to improve the quality of catalytically cracked material.
The characteristics of process integration of the present invention are the solvent of lubricating oil Extract as the extracting wax tailings, to reduce the content of heavy aromatics, colloid and basic nitrogen compound in the wax tailings.
Process integration of the present invention comprises the following steps:
(1) coking raw material is through heating laggard coking tower coking, and coker distillate advances separation column and fractionates out wax tailings;
(2) lube stock and solvent counter-current extraction in the lubricating oil extraction tower, cat head gets the lubricating oil raffinate, gets the lubricating oil Extract at the bottom of the tower;
Characteristics of the present invention are:
(3) with the lubricating oil Extract that obtains of (2) step with obtain wax tailings counter-current extraction in the wax tailings extractor by (1) step, the lubricating oil Extract: wax tailings (calling agent-oil ratio in the following text) is 0.2～5.0: 1, be preferably 0.3～3.0: 1,50～90 ℃ of head temperature, column bottom temperature is 40～70 ℃, cat head goes out the wax tailings raffinate, gets the wax tailings Extract at the bottom of the tower:
(4) the wax tailings raffinate with (3) step reclaims, and the raffinate oil that obtains is made catalytically cracked material, and solvent is used for the lubricating oil extracting and recycles;
(5) the wax tailings Extract with (3) step reclaims, the oil circulation coking of the extraction that obtains, and solvent is used for the lubricating oil extracting and recycles.
Above-mentioned steps (3) can also adopt the settled way of static mixing to be about to the wax tailings that (1) step obtains and the lubricating oil Extract that is obtained by (2) step mixes in static mixer, it is settlement separate to enter slurry tank then, 60～90 ℃ of mixing temperatures, 50～80 ℃ of settling temperature, 0.5～4 hour settling time, best 1～2 hour, the lubricating oil Extract is 0.2～5: 1 with wax tailings mixed weight ratio, best 0.3～3: 1, slurry tank ejects the wax tailings raffinate, and a jar end gets the wax tailings Extract.
Described lubricating oil Extract is being squeezed into an amount of water with the wax tailings counter-current extraction or before mixing, and with control wax tailings raffinate oil yield and quality, the weight ratio of water and lubricating oil Extract (calling the aqua ratio in the following text) is 0.02～0.3: 1.
Described lubricating oil Extract comprises the atmosphere 3rd side cut of any crude oil, normal four lines, vacuum 1st side cut～subtract four lines or the Extract of lube stock after the mixture extracting of phenol, furfural, N-Methyl pyrrolidone or its water light, heavy deasphalted oil.
Described wax tailings can be the wax oil that vacuum residuum, catalytic slurry or its mixture of any crude oil obtains through coking.
Described wax tailings extractor can be packing tower, rotating disc contactor, sieve-tray tower.
Below in conjunction with accompanying drawing characteristics of the present invention are described.
Fig. 1 is lubricating oil Extract and wax tailings counter-current extraction flow process.
Fig. 2 is lubricating oil Extract and wax tailings static mixing sedimentation flow process.
By shown in Figure 1, coking raw material is heated to the coking temperature by pipeline 1 through heating furnace 2 The degree, enter coking tower 4,5 by pipeline 3, the gas products 6 after the coking, 7 by Pipeline 8 enter coking fractional distillation column 9 and with fresh coking raw material 10 heat exchange fractionation, fractionation After tower at the bottom of heavy oil fraction 13 and fresh coking raw material and following from retracting device 27 Ring oil send heating furnace 2 heating, coking from pipeline 1; Cat head and top distillate 11, 12 obtain gas, gasoline and diesel oil after condensation, cooling; The coking that distillates in the tower Wax oil cut 14 advances wax tailings extractor 15. Lube stock 16 is by the lubricating oil extracting Tower 17 bottoms enter, and solvent 18 enters from tower 17 tops with lube stock 16 adverse currents and extracts Get, lubricating oil raffinate 19 enters retracting device 27, and lubricating oil raffinate oil 20 goes out dress Put, solvent 21 recycles; Lubricating oil Extract 22 advances wax tailings extractor 15 Extracting wax tailings 14, wax tailings raffinate 23 enter retracting device 27 and get coking Wax oil raffinate oil 24 is made catalytically cracked material, and solvent 21 recycles; Wax tailings Extract 25 enters retracting device 27, and the wax tailings after the recovery is extracted oil 26 out through pipe Line 1, the circulation coking, solvent 21 recycles. In order to regulate the wax tailings raffinate oil Yield and quality are in lubricating oil Extract 22 pipelines or wax tailings extractor 15 Squeeze into a certain proportion of water.
By shown in Figure 2, this flow process and Fig. 1 difference are in the coking fractional distillation column 9 The lubricating oil that wax tailings cut 14 and the lubricating oil extraction tower 17 that section distillates obtains is taken out Fluid 22 is advanced settling tank 15 again and is separated after static mixer 29 mixes, To wax tailings raffinate 23 and Extract 25 advance respectively retracting device 27. For transferring Yield and the quality of joint wax tailings raffinate oil equally can be to the lubricating oil Extracts Squeeze into a certain proportion of water in 22 pipelines.
Advantage of the present invention:
1, owing to adopt coking and lubricating oil extraction device process integration, use lubricated The oil Extract is directly as extraction wax tailings solvent, the therefore unnecessary cover of building in addition Extraction device, only need former Lubricating oil refining device increase necessary tower, pump, Pipelines etc. can be saved great amount of investment, and have reduced the consumption of novel solvent and return The operating cost of receiving.
2, owing to being dissolved in lubricating oil, the aromatic hydrocarbons in the wax tailings, colloid etc. extract out In the liquid, destroyed the equilibrium relation of Extract, made wherein that saturated hydrocarbons is replaced to come out As catalytically cracked material, therefore, the saturated hydrocarbons in the extract oil of lubricating oil can obtain Rationally utilize.
3, adopt technology of the present invention, wax tailings raffinate oil yield is higher, with Neat solvent relatively, the raffinate oil yield is high by 10 reaching in the situation of equal basic nitrogen More than the m%.
4, technology of the present invention can significantly reduce wax tailings alkali nitrogen and colloid contains Amount is for catalytic cracking unit provides quality raw materials.
Further describe characteristics of the present invention with example below.
Example 1
This example is on the packaged unit of treatment capacity 1400g/h, uses the lubricating oil Extract to the wax tailings extraction test.Adopt LIAOHE CRUDE to subtract phenol Extract and furfural Extract extraction LIAOHE CRUDE vacuum residuum wax tailings that three-way lube stock obtains after the extracting respectively through phenol, furfural solvent.Test conditions and the results are shown in subordinate list.
As shown in Table 1, when adopting lubricating oil Extract extraction wax tailings, raffinate oil dealkalize nitrogen rate is up to 75.0%, saturated hydrocarbon content, H/C atomic ratio all improve a lot, gum level significantly reduces, and the raffinate oil yield has improved the quality and the yield of catalytically cracked material significantly up to 99.7%.
Example 2
This example is to test with Fig. 2 static mixing sedimentation process of the present invention.Adopt wax tailings raw material and the lubricating oil Extract same with example 1, its test conditions and result are shown in subordinate list.
By table 1 data as can be known, adopt the mixing sedimentation process to have equally and remove alkali nitrogen and colloid effect significantly, and wax tailings raffinate oil yield is also very high.Therefore the static mixing sedimentation process can provide more fine catalytically cracked material equally.
Example 3
The USP4534854 technical process of this example on the device identical with example 1, extracts same wax tailings raw material respectively with phenol and furfural solvent.Test conditions and the results are shown in subordinate list.
Example 1 and example 2 can be drawn with example 3 contrasts:
1. when wax tailings raffinate oil alkali nitrogen content reaches par, higher more than 10% than the raffinate oil yield of USP4534854 process using novel solvent extraction wax tailings with lubricating oil Extract extraction wax tailings.
2. as can be seen from viscosity, density and the compositional analysis data of wax tailings raw material and wax tailings raffinate oil, lubricating oil is extracted some components in the oil out, particularly stable hydrocarbon etc. turns back in the wax tailings raffinate oil as catalytically cracked material, makes lubricating oil extract oil out and is fully used.
Subordinate list
Claims (8)
1, a kind of process integration of producing fine quality catalytic cracking raw material oil comprises the following steps: (1) coking raw material through heating laggard coking tower coking, and coker distillate advances separation column and fractionates out wax tailings; (2) lube stock and solvent counter-current extraction in the lubricating oil extraction tower, cat head gets the lubricating oil raffinate, get the lubricating oil Extract at the bottom of the tower, the present invention is characterised in that: (3) are with (2) step lubricating oil Extract that obtains and the wax tailings counter-current extraction in the wax tailings extractor that is obtained by (1) step, cat head goes out the wax tailings raffinate, get the wax tailings Extract at the bottom of the tower, (4) the wax tailings raffinate with (3) step reclaims, the raffinate oil that obtains is made catalytically cracked material, solvent return (2) step recycle, (5) the wax tailings Extract with (3) step reclaims, and the extraction oil that obtains is got back to (1) step circulation coking, and solvent returns (2) step and recycles.
2, according to the described process integration of claim 1, it is characterized in that step (3) can also mix wax tailings and lubricating oil Extract in static mixer, it is settlement separate to advance slurry tank then, 60～90 ℃ of mixing temperatures, 50～80 ℃ of settling temperature, 0.5～4 hour settling time, tank deck goes out the wax tailings raffinate, and a jar end goes out the wax tailings Extract.
3, according to claim 1 or 2 described technologies, it is characterized in that the lubricating oil Extract squeezes into an amount of water with the wax tailings counter-current extraction or before mixing, the weight ratio of water and lubricating oil Extract is 0.02～0.3: 1.
4,, it is characterized in that step (3) lubricating oil Extract and wax tailings weight ratio are 0.2～5: 1,50～90 ℃ of extractor head temperature, 40～70 ℃ of bottom temps according to the described technology of claim 1.
5,, it is characterized in that described wax tailings extractor is packing tower, rotating disc contactor or sieve-tray tower according to the described technology of claim 1.
6,, it is characterized in that lubricating oil Extract and wax tailings mixed weight ratio are 0.2～5: 1 according to the described technology of claim 2.
7,, it is characterized in that described lubricating oil Extract comprises atmosphere 3rd side cut, normal four lines, vacuum 1st side cut～subtract four lines or the Extract of lube stock after the mixture extracting of phenol, furfural, N-Methyl pyrrolidone or its water light, heavy deasphalted oil according to claim 1 or 2 described technologies.
8,, it is characterized in that described wax tailings is the wax oil that vacuum residuum, catalytic slurry or its mixture obtain through coking according to claim 1 or 2 described technologies.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN95103679A CN1058514C (en) | 1995-04-11 | 1995-04-11 | Combination process for producing fine quality catalytic cracking raw material |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN95103679A CN1058514C (en) | 1995-04-11 | 1995-04-11 | Combination process for producing fine quality catalytic cracking raw material |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1133338A CN1133338A (en) | 1996-10-16 |
| CN1058514C true CN1058514C (en) | 2000-11-15 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN95103679A Expired - Fee Related CN1058514C (en) | 1995-04-11 | 1995-04-11 | Combination process for producing fine quality catalytic cracking raw material |
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| Country | Link |
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| CN (1) | CN1058514C (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114177655B (en) * | 2021-12-23 | 2023-03-10 | 安徽国孚凤凰科技有限公司 | Fiber separation type saturated oil separation recovery device and method for base oil solvent extraction extract liquid |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4454023A (en) * | 1983-03-23 | 1984-06-12 | Alberta Oil Sands Technology & Research Authority | Process for upgrading a heavy viscous hydrocarbon |
| US4528088A (en) * | 1983-11-30 | 1985-07-09 | Exxon Research And Engineering Co. | Coking with solvent separation of recycle oil using coker naphtha and solvent recovery |
| US4534854A (en) * | 1983-08-17 | 1985-08-13 | Exxon Research And Engineering Co. | Delayed coking with solvent separation of recycle oil |
-
1995
- 1995-04-11 CN CN95103679A patent/CN1058514C/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4454023A (en) * | 1983-03-23 | 1984-06-12 | Alberta Oil Sands Technology & Research Authority | Process for upgrading a heavy viscous hydrocarbon |
| US4534854A (en) * | 1983-08-17 | 1985-08-13 | Exxon Research And Engineering Co. | Delayed coking with solvent separation of recycle oil |
| US4528088A (en) * | 1983-11-30 | 1985-07-09 | Exxon Research And Engineering Co. | Coking with solvent separation of recycle oil using coker naphtha and solvent recovery |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1133338A (en) | 1996-10-16 |
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